Process for use of molecular sieve adsorbent blends

ABSTRACT

A Process for the production and uses of a molecular sieve adsorbent blend product with improved performance characteristics produced by preparing a zeolite powder, preparing a highly dispersed attapulgite fiber binder, mixing the zeolite powder with the highly dispersed attapulgite binder to form a mixture, forming molecular sieve adsorbent products into a shaped material and calcining the shaped material, wherein the tapped bulk density of the highly dispersed attapulgite fibers measured according to DIN/ISO 787 is more than about 550 g/ml.

CROSS REFERENCE TO RELATED APPLICATIONS

This application is a divisional application based on application Ser.No. 10/054,041, filed on Jan. 22, 2002 now U.S. Pat. No. 6,743,745.

BACKGROUND OF INVENTION

1. Field of Invention

This invention relates to molecular sieve adsorbents and moreparticularly to processes of use of a molecular sieve adsorbent blendcomprising a zeolite and a highly dispersed attapulgite binder. Thisinvention also relates to processes of use of molecular sieve adsorbentblends prepared by the process of blending a zeolite with a highlydispersed attapulgite binder.

2. Background Art

Zeolites are hydrated metal alumino silicates having the general formulaM_(2/n)O:Al₂O₃:xSiO₂:yH₂Owhere M usually represents a metal of the alkali or alkaline earthgroup, n is the valence of the metal M, x varies from 2 to infinity,depending on the zeolite structure type and y designates the hydratedstatus of the zeolite. Most zeolites are three-dimensional crystals witha crystal size in the range of 0.1 to 30 μm. Heating these zeolites tohigh temperatures results in the loss of the water of hydration, leavinga crystalline structure with channels of molecular dimensions, offeringa high surface area for the adsorption of inorganic or organicmolecules. Adsorption of these molecules is limited by the size of thezeolite channels. The rate of adsorption is limited by the laws ofdiffusion.

One limitation on the utilization of these zeolite crystals is theirextremely fine particle size. Large naturally-formed agglomerates ofthese crystals break apart easily. Because the pressure drop through thebed is prohibitively high, these zeolite crystals cannot be used infixed beds for various dynamic applications, such as drying of naturalgas, drying of air, separation of impurities from a gas stream,separation of liquid product streams and the like. Therefore, it isdesirable to agglomerate these crystals with other materials to providean agglomerate mass of the crystals which exhibits a reduced pressuredrop.

To permit the utilization of these molecular sieve crystals, differenttypes of clays are used as binders including attapulgite, palygorskite,kaolin, sepiolite, bentonite, montmorillonite and mixtures thereof. Forexample, U.S. Pat. No. 2,973,327 discloses the use of a number ofdifferent types of clays, including attapulgite, as a binder formolecular sieves. The clay content of the bonded molecular sieve canvary from as low as 1 percent to as high as 40 percent by weight,although the preferred range is from about 10 to about 25 percent byweight.

U.S. Pat. No. 3,219,590 discloses another molecular sieve blendcomprising a kaolin-type clay and a lignosulfonate which functions asthe binding agent.

Adsorbent materials comprising a type 5A zeolite molecular sieve and akaolin clay binder, wherein the kaolin comprise from about 10 to about40 percent of the composition, are disclosed in U.S. Pat. No. 5,001,098.

Molded bodies containing dealuminated zeolite Y and a binder materialare disclosed in U.S. Pat. No. 5,316,993.

An adsorbent and/or catalyst blended with a binder system comprising acolloidal metal oxide, an oxide adsorbent and an acid are disclosed inU.S. Pat. No. 5,948,726.

An adsorbent for separating gases comprising a binder and a crystalline,low silica faujasite-type zeolite with a silica to alumina molar ratioof 1.9 to 2.1 is disclosed in EP 0 940 174 A2. This reference disclosesthe blending of a zeolite with a conventional, dense attapulgite claybinder useful for the separation of gases. The bulk density of thebinder is not disclosed.

Another blend of a conventional, dense attapulgite clay binder with azeolite is disclosed in U.S. Pat. No. 5,413,978. The bulk density of theattapulgite clay is from about 400 g/l to about 530 g/l.

An abrasion-resistant granular zeolite formed by blending a zeolite anda binder system is disclosed in U.S. Pat. No. 4,420,419. See also U.S.Pat. No. 5,292,360 which discloses an adsorbent for the purification ofgases comprising a 5A zeolite molecular sieve and a kaolin clay binder.

One problem with conventionally formed zeolite blends is decreaseddiffusion. The larger the diameter of the formed zeolites, the slowerthe rate of diffusion of the molecules to be adsorbed. Particularly inthe field of pressure swing adsorption, this effect is highly adverse toshort cycle time and thus to productivity. Enhanced kinetic values orfaster mass transfer rates can result in shorter cycle time and lowerpower consumption and thus higher adsorbent productivity.

It has been recognized that a reduction in the particle size of formedzeolites leads to shorter mass transfer zones and shorter cycle times.This is based on the assumption that the time needed for adsorbates totravel through the macropores of the adsorbents limits the cycle time,i.e. macropore diffusion is the rate limiting step in these processes.This problem can be improved by adding pore forming compounds to thezeolite clay blend before the forming step.

Accordingly it is an object of the invention to disclose a process forthe preparation of molecular sieve adsorbents with enhanced diffusionrates.

It is a still further object of the invention to disclose a process forthe production of a molecular sieve adsorbent blend which is especiallyuseful in thermal swing adsorption (TSA) systems and in pressure swingadsorption (PSA) systems.

It is a still further object of the invention to disclose molecularsieve adsorbent blends which maintain their physical properties anddiffusion capabilities even with reduced binder percentages.

It is a still further object of the invention to disclose a process forthe production of a molecular sieve adsorbent blend utilizing highlydispersed attapulgite fibers.

It is a still further object of the invention to disclose a molecularsieve adsorbent blend comprising a zeolite powder and a highly dispersedattapulgite binder.

It is a still further object of the invention to disclose a process fordrying a feed stream comprising passing the feed stream over a molecularsieve adsorbent blend comprising a zeolite and a highly dispersedattapulgite binder.

It is a still further object of the invention to disclose a process forthe adsorption of carbon dioxide from an air stream comprising passingthat air stream over a molecular sieve adsorbent blend comprising azeolite powder and a highly dispersed attapulgite binder.

It is still further object of the invention to disclose a process forseparation of components of a gaseous or liquid feed stream comprisingpassing that gaseous or liquid feed stream over a molecular sieveadsorbent blend comprising a zeolite powder and a highly dispersedattapulgite binder.

These and other objects are obtained by the process for production, theprocess for use and product of the invention disclosed herein.

SUMMARY OF THE INVENTION

The present invention is a process for the production of a molecularsieve adsorbent blend with improved performance characteristicscomprising

-   -   preparing a zeolite,    -   preparing an attapulgite binder containing highly dispersed        attapulgite fibers,    -   mixing the zeolite with the attapulgite binder in an aqueous        mixture,    -   forming molecular sieve adsorbent products from the mixture, and    -   calcining the adsorbent product to form a molecular sieve        adsorbent blend, wherein the tapped bulk density of the highly        dispersed attapulgite fibers, is above 550 g/l as measured        according to DIN/ISO 787, and wherein the water adsorption        capacity of the highly dispersed binder is above 35 percent        (w/w).

The present invention is also a molecular sieve adsorbent blendcomprising

-   -   a zeolite blended with a highly dispersed attapulgite binder,        wherein the tapped bulk density of the highly dispersed        attapulgite binder is above 550 g/l as measured according to        DIN/ISO 787, and wherein water adsorption capacity of the highly        dispersed binder is above 35 percent (w/w).

The present invention is also a process for drying a feed streamcomprising passing the feed stream over a molecular sieve adsorbentblend comprising a zeolite blended with a highly dispersed attapulgitebinder as defined above.

The invention is also a process for the separation of components of agaseous or liquid feed stream comprising passing the liquid feed streamover a molecular sieve adsorbent blend comprising a zeolite blended witha highly dispersed attapulgite binder as defined above.

DETAILED DESCRIPTION OF THE INVENTION

The present invention is a molecular sieve adsorbent blend formed from azeolite blended with a highly dispersed attapulgite binder and a processfor formation of that product. The invention is based on the discoverythat the adsorption rate of a molecular sieve product is not onlydependent upon the size of the formed zeolite particles, but also thetype and characteristics of the binder blended with the zeolite. It hasbeen surprisingly discovered that the same type and quantity of zeolitewhen blended with different binders produces zeolite blends whichexhibit different adsorption characteristics depending upon the binderthat is used. The phrase “adsorption rate” or “sorption rate” or “masstransfer rate” means the rate at which an adsorbate loading in a feedstream changes over a given period of time for a given adsorptionseparation process.

The prior art suggests that the adsorption rate of a molecular sieveadsorbent is only a function of the porosity and particle size of themolecular sieve adsorbent. It has now been surprisingly discovered thatthe type of binder that is used to bind the zeolite crystals also playsa role in the adsorption rate of the zeolite material.

Adsorbent aggregates or blends are formed by mixing zeolite crystalswith binder materials. Various types of zeolites may be used to form theadsorbent blend including zeolite A, zeolite X, zeolite Y, zeoliteZSM-5, zeolite Beta, synthetic mordenite and blends thereof. Thesezeolites may be used singly or in mixtures of two or more zeolites.Zeolites may be present in their alkali or alkaline earth metalsubstituted form. The particular type of zeolite present in the blenddepends upon the adsorbate that is to be adsorbed from the feed stream.For example, when the desired adsorbent is carbon dioxide in a gasstream, the preferred zeolites include zeolite X or zeolite LSX. Whenthe adsorption process is for the purification of gases, notably bypressure swing adsorption (PSA) and temperature swing adsorption (TSA)methods, the preferred zeolites include zeolite A or zeolite X.

Binder materials are utilized to bind the individual zeolite crystalstogether, to form shaped products and to reduce the pressure drop duringadsorption. However, in the past the binder material has not enhancedthe adsorption capability of the zeolite. In fact, conventional bindermaterials have generally reduced the adsorption capacity of thezeolites. Binder materials which have been utilized with zeolites in thepast include clay minerals, such as kaolin, palygorskite-type minerals,such as attapulgite, and smectite-type clay minerals, such asmontmorillonite or bentonite. These clay binders have been used singlyor in mixtures of two or more different types of clay binders.

The inventors have discovered that a particularly useful blend ofzeolites and a clay binder is produced when the clay material is anattapulgite clay which has been “highly dispersed.” Generally speaking,clay particles, especially attapulgite clay particles, exist as densematerials with very limited adsorption capabilities. These conventionalclay binder particles are different in size and shape from the zeoliteparticles. When blended with zeolite crystals they tend to occupy spacebetween the zeolite crystals and may assist in the adsorption by thezeolite material without increasing the overall adsorption of thezeolite blend.

In particular, attapulgite clay particles, even after mining andwork-up, are naturally formed in the shape of dense bundles of clumpedbristles. The existence of these bundles has been confirmed usingscanning electron microscopy (SEM). These bristles must be separated orground to permit their use as binders for zeolite particles. Withoutgrinding these attapulgite clay particles to a smaller size, anon-porous layer of attapulgite clay particles is created in the zeoliteblend, preventing or substantially limiting, diffusion of adsorbatesthrough the blend. The conventional attapulgite clays that have beenutilized in the past are produced by dry grinding the attapulgite clay.In the conventional process these dry ground attapulgite clay bundles ofbristles are then blended with the zeolite crystals. However, even afterthis conventional grinding of the attapulgite clay bundles, largebundles of attapulgite clay bristles are still present. When theseconventional attapulgite clay bundles are blended with zeolite andformed into adsorbents, the capability of the zeolite materials toadsorb the desired adsorbate is not substantially enhanced.

The applicants' invention utilizes “highly dispersed” attapulgite clayas the binder material that is blended with the zeolite powder. Thedifference between conventional, dense attapulgite clay bundles and the“highly dispersed” attapulgite clay particles of the invention can bedifferentiated readily through the use of a scanning electronmicroscopy. Another method to distinguish between conventional denseattapulgite clay and the “highly dispersed” attapulgite clay products ofthe invention is by the use of tapped bulk density measurement asdetermined according to DIN/ISO 787. Dense attapulgite clay binderscontain a residual water content of about 20-25 percent and have atapped bulk density of about 400 g/l to about 530 g/l. “Highlydispersed” attapulgite binders also contain residual water of about20-25 percent but have a tapped bulk density of about 550 g/l to about700 g/l.

Another method to distinguish between conventional dense attapulgiteclay and highly dispersed attapulgite clay products of the invention isby determining the water adsorption capacity of the attapulgite clayproducts. To determine whether the clay binder is “highly dispersed” theclay binder is fully saturated at 50 percent relative humidity at 25° C.to the point where an equilibrium adsorption capacity is achieved. Thisprocess may take up to 72 hours. After full hydration of the clay isachieved the clay is dried at 550° C. for at least two hours. Thedifference of the weight between the fully hydrated clay and the driedclay is the water adsorption capacity. For dense attapulgite clays, thewater adsorption capacity is below 30 percent whereas for the “highlydispersed” attapulgite clay, the water adsorption capacity is above 35percent.

While any process which produces attapulgite fibers which are “highlydispersed” as defined above is within the scope of the invention, onepreferred process is disclosed in U.S. Pat. No. 6,130,179, the contentsof which are incorporated by reference into this application. Thispatent fails to disclose or suggest the use of this highly dispersedattapulgite clay with zeolite. The process of U.S. Pat. No. 6,130,179utilizes a dispersant which disperses the individual attapulgiteparticles in water such that they remain in suspension even after othermaterials, including other clay and mineral species, are removed fromthat solution. Once the “highly dispersed” attapulgite clay is prepared,it is ready for use in the production of the molecular sieve adsorbentproduct of the invention.

Generally the process to produce the molecular sieve adsorbent blendproduct with improved performance characteristics according to theinvention is as follows:

-   -   prepare the zeolite material,    -   prepare an attapulgite binder comprising highly dispersed        attapulgite fibers,    -   mix the zeolite with the attapulgite binder in an aqueous        mixture,    -   form an uncalcined material from the mixture, and    -   calcine the material to form the molecular sieve adsorbent blend        product of the invention.

Once the appropriate zeolite material is chosen for a given application,it is mixed with the highly dispersed attapulgite binder in the presenceof water. The zeolite powder and the highly dispersed attapulgite binderare blended together with water. The amount of highly dispersedattapulgite binder that is utilized can range from 5 to about 30 percentby weight, preferably from about 5 to about 20 percent and mostpreferably in the range of about 10 percent of the blend. Conventionalmixtures of zeolite and non-highly dispersed attapulgite clay bindersutilize about 20 percent or more attapulgite clay. Sufficient water isretained in or added to the mixture to make a formable mixture, i.e.,one that can be easily extruded.

The mixture is blended using a conventional blending device, such as aconventional mixer, until a mass of suitable viscosity for forming isobtained. The blended mixture is then formed into the appropriate shapedproduct, for example, by extrusion. The products can be formed in anyconventional shape such as beads, pellets, tablets or other suchconventional shaped products. Once the formed products are produced intothe appropriate shape, they are calcined, preferably at about 600° C.,for about 30 minutes to 2 hours.

In an optional preferred embodiment, a pore forming agent may be addedto the zeolite/attapulgite clay mixture during the mixing step toenhance the total pore volume of the end product. Among the acceptablepore forming agents are fibers, including rayon, nylon, sisal, flax andthe like and organic polymers, including corn starch, starchderivatives, lignosulfonates, polyacrylamide, polyacrylic acid,cellulose, cellulose derivatives and the like. The amount of the poreforming agent that may be added is from about 2 to about 15 percent, byweight.

Products produced by the process of the invention show improvedadsorption rates. The adsorption rate can be determined using severaldifferent methods. For example, in one preferred process, the adsorbentproduct produced according to the invention can be tested to determinethe time necessary to achieve 95 percent of the maximum adsorptioncapacity of the material. The shorter the time to achieve this value,the faster the adsorption rate.

In another process to determine the adsorption rate of the molecularsieve adsorbent blend of the invention, the amount of the adsorbedproduct that has been adsorbed over a given period of time can bedetermined.

In a further process of comparison of adsorption, the mass transfer zoneof the blend of the invention can be compared to that of a conventionalblend under given conditions. The shorter the mass transfer zone, thehigher the adsorption rate.

Finally, the diffusion rate can be determined directly for certain gasesor liquids. The higher the diffusion rate, the faster the adsorptionrate.

It has been surprisingly discovered that by replacing a conventionalattapulgite binder with the same quantity of “highly dispersed”attapulgite binder of the invention, there is an improved adsorptionrate regardless of which method is used to measure that rate. Theimprovement in adsorption rate is at least about 10 percent and as highas 200 percent compared to products containing conventional attapulgiteclay binders. This improvement is especially important because of theincreased cost of the highly dispersed attapulgite binder overconventional attapulgite binders.

A further surprising improvement is in the ability of the zeoliteadsorbent blend product to maintain its crush strength even when theamount of the attapulgite binder that are added to the mixture isreduced. Generally speaking, the more binder that is present in theforming process, the better the crush strength for the finished product.For conventional dense attapulgite binders, this improvement in thecrush strength is dramatic when the percentage of attapulgite binderwithin the end product increases from zero to about 20 percent of thecomposition. Products made with conventional dense attapulgite binder of10 percent or less are not practical as their crush strength drops belowacceptable levels. It has been surprisingly discovered that a productproduced using the highly dispersed attapulgite fibers of the inventionproduces an end product with adequate crush strength even when thequantity of the highly dispersed attapulgite binder in the end productis as low as 10 percent or less. Further, at any particular percentageof binder material, the crush strength of a product produced using thehighly dispersed attapulgite fiber of the invention is higher than for aproduct made with a conventional dense attapulgite binder.

It has also been surprisingly discovered that even when lowerpercentages of a highly dispersed attapulgite fiber are utilized in anadsorbent product, the rate of water adsorption increases. This isevidenced by a reduction in the amount of time that is necessary toachieve a particular predetermined amount to be adsorbed. Thisimprovement is at least 10 percent and in many cases as much as 30percent or more.

The highly dispersed attapulgite binder can be blended with zeolite andused for a number of different processes. For example, the blend ofhighly dispersed attapulgite clay and zeolite can be used for drying afeed stream, such as for the removal of water from a gaseous or liquidethanol stream. The blend can also be used for the separation ofnitrogen from an air stream. Further, the blend can be used for theremoval of sulfur and oxygen containing compounds from a hydrocarbonstream. Another use for this blend is for the removal of carbonmonoxide, carbon dioxide and nitrogen from a hydrogen gas stream. Theblend can also be used for the removal of water from a gaseous or liquidhydrocarbon stream or for the removal of water from a gaseous or liquidstream of refrigerants. Another use is for the removal of water andcarbon dioxide from air. The adsorbent material of the invention mayalso be used for the separation of organic compound, such as for theseparation of n-paraffins from a mixture of iso-paraffins andn-paraffins or for the conversion of certain organic compounds. Thereare a number of other processes for which this blend of a highlydispersed attapulgite clay and zeolite can be utilized which would bewell known to a person skilled in the art and which are covered by thisinvention.

These improvements are shown by the following examples:

EXAMPLES Example 1

Samples of an attapulgite clay material that is conventionally used as abinder for zeolites and a highly dispersed attapulgite clay materialwere tested for tapped bulk density, residual water and water adsorptioncapacity. Tapped bulk density was determined according to DIN/ISO 787.(Actigel 208 obtained from ITC Floridin was used as the highly dispersedattapulgite clay in all examples. The conventional attapulgite clayswere of different brands and obtained from ITC Floridin.)

A clay sample of about 10 grams was weighed in a porcelain crucible(weighing precision 1 mg) and heated to 550° C. for 2 hours. The samplewas cooled to room temperature in a desiccator and weighed (weighingprecision 1 mg). The weight difference led to the residual water amount.

Another clay sample of about 10 grams was weighed in a porcelaincrucible (weighing precision 1 mg) and was water saturated at 50 percentrelative humidity and 20° C. The equilibrium was reached within 72hours. The sample was weighed (weighing precision 1 mg) and heated to550° C. for 2 hours. The sample was cooled to room temperature in adesiccator and weighed (weighing precision 1 mg). The weight differenceof the fully hydrated sample and fully dried sample led to the wateradsorption capacity given in Table 1 below. The fully dried mass wastaken as 100 percent clay.

TABLE 1 Attapulgite Clay Sample Highly Conventional ConventionalConventional Dispersed Dense Dense Dense Clay Clay 1 Clay 2 Clay 3Tapped Bulk 617 398 + 31 529 + 20 428 Density (g/ml) 595 (average of(average of 459 660 17 samples) 21 samples) Residual Water 22.3 25.521.4 25.5 as Received (%) 21.7 22.6 23.7 Water 36.8 28.8 25.0 29.7Adsorption 36.0 28.8 Capacity (%) 36.0

As is clear from the Table, the bulk density of the highly dispersedclay was significantly higher than the bulk density of the conventionaldense attapulgite clay. In addition, the water adsorption capacity ofthe highly dispersed attapulgite clay was significantly higher than thatof the conventional dense attapulgite clay.

Example 2

The crush strength of samples of a molecular sieve adsorbent blendproduct prepared using a conventional dense attapulgite clay wascompared with a molecular sieve adsorbent blend product prepared using ahighly dispersed attapulgite clay.

To determine the crush strength of the various samples, molecular sieveblends were prepared. Sodium A molecular sieve was blended with variousamounts of both a conventional dense attapulgite clay and the highlydispersed attapulgite clay. To 100 grams of the molecular sieve/claybinder mixture about 30 to 40 grams of water were added and then blendedfor up to 180 minutes using a conventional blender. The product was thenextruded in the form of {fraction (1/16)}″ extrudates. These extrudateswere then dried at approximately 120° C. for 8 to 12 hours and thencalcined at 600° C. for about 2 hours.

TABLE 2 Crush Strength in Relation to the Amount of Binder UsedConventional Conventional Conventional Highly Highly Highly Dense DenseDense Dispersed Dispersed Dispersed Binder Binder Binder Binder BinderBinder (20%) (15%) (10%) (20%) (15%) (10%) Size of {fraction (1/16)}″{fraction (1/16)}″ {fraction (1/16)}″ {fraction (1/16)}″ {fraction(1/16)}″ {fraction (1/16)}″ Extrudates Crush 19.9 8.8 7.5 28.5 19.6 16.1Strength [N]

Surprisingly the crush strength of a product made with 20 percent highlydispersed attapulgite fibers was significantly greater than a productmade with the same percentage of a conventional dense attapulgitebinder. Further, the crush strength remained at a reasonably high leveleven when the amount of the highly dispersed attapulgite fiber wasreduced to 10 percent, whereas the crush strength of the material usingthe conventional attapulgite binder dropped rather significantly.

Example 3 Water Adsorption Kinetics

The materials prepared in Example 2 were tested for water adsorptionkinetics. It was surprisingly discovered that the amount of binder didnot have an impact on the water adsorption kinetics of the material madewith the conventional binder. In contrast, it was surprisinglydiscovered that when the amount of the highly dispersed attapulgitefiber was reduced to 10 percent, the rate of adsorption of water toreach 95 percent of adsorption capacity increased dramatically. Detailsare shown in the attached Table 3.

TABLE 3 Influence of Binder Type and Binder Amount to Water AdsorptionKinetics Conventional Conventional Conventional Highly Highly HighlyDense Dense Dense Dispersed Dispersed Dispersed Binder Binder BinderBinder Binder Binder (20%) (15%) (10%) (20%) (15%) (10%) Size of{fraction (1/16)}″ {fraction (1/16)}″ {fraction (1/16)}″ {fraction(1/16)}″ {fraction (1/16)}″ {fraction (1/16)}″ Extrudates H₂O 121 130122 136 133 96 Adsorption Kinetics at 1 mbar [min]

Example 4 Beaded Molecular Sieve 3A

A premixed zeolite 3A powder/attapulgite clay composition was addedcontinuously to a granulation pan. The zeolite 3A powder was acquiredfrom CU Chemie Uetikon AG. During the beading process, water was sprayedon the powder mixture to maintain a constant humidity. The powdermixture was added at a speed of 300 kg/hr. After having finished theaddition of the powder mixture, the beads were rolled for another 10minutes. The green beads were dried at 100° C. and then calcined at 600°C. The calcined beads were stored in well closed containers andanalyzed. Table 4 gives the comparative results for the two differentbeaded materials. While physical properties, such as crush strength andbulk density were generally the same for both samples, mass transferzone was reduced significantly and water adsorption rate wassurprisingly faster for the product made with the highly dispersedattapulgite clay.

TABLE 4 Comparative Results of a Conventional 3A Molecular Sieve and aMolecular Sieve Produced with 10% Highly Dispersed Attapulgite Clay as aBeneficiated Attapulgite Binder Reference According to Material (20%Invention (10% Dense Attapulgite Highly Dispersed Binder) AttapulgiteClay) Bead Size [mesh] 4 × 8 4 × 8 Crush Strength [N] 51 46 Bulk Density[g/l] 721 687 Water Adsorption 20.1 21.3 50% r.h. [%] Water MassTransfer 253 167 Zone [mm] Water Adsorption 184 105 Kinetic (time toreach 95% ads. capacity; 4 mbar) [min]

Example 5 Beaded Molecular Sieve 3A for Natural Gas Drying

A premixed zeolite 3A powder/organic additive/clay composition was addedcontinuously to a granulation pan. During the beading process, water wassprayed onto the powder mixture to keep a constant humidity. The powdermixture was added at a speed of 300 kg/hr. After having finished theaddition of the powder mixture, the beads were rolled for another 10minutes. The green beads were dried at 100° C. and then calcined at 630°C. The calcined beads were stored in closed containers and analyzed. Theamount of organic additive was kept constant for both experiments. Table5 gives the comparative results of the two different beaded materials.While physical properties, attrition, and bulk density are generally thesame for both samples, water adsorption rate increased surprisingly forthe product produced using the highly dispersed attapulgite clay. Thebeads are much smaller than in Example 4, but the increase in theadsorption rate was still very high, indicating that the effect isintrinsic.

TABLE 5 Comparative Results of a Conventional 3A Molecular Sieve Usedfor Natural Gas Drying and a Molecular Sieve Produced with 10% HighlyDispersed Attapulgite Clay as a Beneficiated Attapulgite ReferenceMaterial According to (20% Conventional Invention (10% Dense AttapulgiteHighly Dispersed Binder) Attapulgite Clay) Bead Size [mesh] 8 × 12 8 ×12 Attrition [%] 0.04 0.02 Bulk Density [g/l] 730 722 Water Adsorption22.2 22.7 50% r.h. [%] Water Adsorption 14.1 18.5 Kinetic at p/p₀ =0.03, after 120 min. [%]

Example 6 Beaded Molecular Sieve 5A

A premixed zeolite 5A powder/clay composition was added continuously toa granulation pan. The zeolite 5A powder was acquired from Zeochem Ltd.During the beading process, water was sprayed onto the powder mixture tokeep a constant humidity. The powder mixture was added at a speed of 300kg/hr. After having finished the addition of the powder mixture, thebeads were rolled for another 10 minutes. The green beads were dried at100° C. and then calcined at 630° C. The calcined beads were stored inclosed containers and analyzed. Table 6 gives the comparative results ofthe two different beaded materials. While butane adsorption capacityincreased within expectations, nitrogen adsorption kinetic increasedsurprisingly, certainly more than was anticipated.

TABLE 6 Comparative Results of a Conventional 5A Molecular Sieve and aMolecular Sieve Produced with 10% Highly Dispersed Attapulgite Clay as aBeneficiated Attapulgite Binder Reference According to Material (20%Invention (10% Conventional Dense Highly Dispersed Attapulgite Binder)Attapulgite Clay) Bead Size [mesh] 8 × 12 8 × 12 N-Butane Adsorption8.0  9.3  Capacity; 1 bar/25° C. [%] Nitrogen Kinetic 0.17 0.39 Value[l/s]

Example 7 Beaded Molecular Sieve 4A

The same preparation procedure was used as in Example 6, except thatzeolite 4A powder acquired from CU Chemie Uetikon was used for thebeading process. The amount of the binder for the new formulation wasincreased to 15%. The drying and the calcination process followed thesame temperature profiles as was used in Example 6. The results aregiven in Table 7. The Example using 15% of the highly dispersedattapulgite binder showed a surprising improvement in the adsorptionrate. The mass transfer zone dropped from 137 mm to 106 mm and the wateradsorption capacity after 120 minutes increased from 15.0% to 17.2%.

TABLE 7 Comparative Results of a Conventional 5A Molecular Sieve and aMolecular Sieve Produced with 15% Highly Dispersed Attapulgite Clay as aBeneficiated Attapulgite Binder Reference According to Material (20%Invention (15% Conventional Dense Highly Dispersed Attapulgite Binder)Attapulgite Clay) Bead Size [mm] 2-3 2-3 Crush Strength [N] 57 41Attrition [%] 0.03 0.01 Bulk Density 729 710 [g/l] Water Mass Transfer137 106 Zone [mm] Water Adsorption 15.0 17.2 Kinetic at p/p₀ (after 120min.) [%]

Example 8 Beaded Molecular Sieve 13X Used for Air Purification and/orfor Air Separation

A premixed zeolite 13X powder/organic additive/clay composition wasadded continuously to a granulation pan. The 13X zeolite powder wasacquired from CU Chemie Uetikon AG. During the beading process, waterwas sprayed onto the powder mixture to keep a constant humidity. Thepowder mixture was added at a rate of 500 kg/hr. After having finishedthe addition of the powder mixture, the beads were rolled for another 10minutes. The green beads were dried at 100° C. and then calcined at 620°C. The calcined and cooled beads were stored in air tight containers andanalyzed. The analytical results of the finished product are given inTable 8. Again, the physical properties remained within expectations,but the adsorption rate increased for the composition of the inventionmuch more than expected, especially for the adsorption of nitrogen.

TABLE 8 Comparative Results of a Conventional 13X Molecular Sieve Usedfor Air Prepurification and for Air Separation, and a Molecular SieveProduced with 10% Highly Dispersed Attapulgite Clay as a BeneficiatedAttapulgite Binder Reference Material According to (16% Dense Invention(10% Conventional Highly Dispersed Attapulgite Binder) Attapulgite Clay)Bead Size [mm] 1.0-2.0 1.0-2.0 Attrition [%] 0.05 0.07 Bulk Density[g/l] 640 638 Water Adsorption 28.1 30.7 Capacity 50% r.h. [%] CO₂Adsorption 12.6 13.6 Capacity 45 mbar/ 25° C. [%] Water Adsorption 17.019.2 Kinetic at p/p₀ = 0.03 (after 120 min.) [%] Nitrogen Kinetic 0.200.33 Value [l/s]

As is shown from these examples, there are surprising improvements inthe performance of molecular sieve adsorbent blends using attapulgitebinder produced from highly dispersed attapulgite fibers. Thisimprovement in crush strength, adsorption kinetics and othercharacteristics as shown in the Examples was surprising and dramatic.

Although the invention has been described in detail, it is clearlyunderstood that the same is by no way to be taken as a limitation. Thescope of the present invention can only be limited by the appendedclaims.

1. A process for separation of components of a gaseous or a liquid feedstream comprising passing the components of the gaseous or liquid feedstream over a molecular sieve adsorbent blend produced by a processcomprising preparing a zeolite product; preparing an attapulgite bindercomprising highly dispersed attapulgite fibers; mixing the zeolite withthe attapulgite binder and water to produce a mixture; and forming amolecular sieve adsorbent product from the mixture; wherein the tappedbulk density of the highly dispersed attapulgite fibers, as measuredaccording DIN/ISO 787, is more than about 550 g/l.
 2. The process ofclaim 1 wherein the zeolite product comprises zeolite X or zeolite A. 3.The process of claim 1 wherein the attapulgite binder comprises fromabout 5 to about 30 percent of the mixture, by weight.
 4. The process ofclaim 1 wherein the attapulgite binder comprises from about 5 to about20 percent of the mixture, by weight.
 5. A process for drying a gaseousfeed stream comprising passing the feed stream over a molecular sieveadsorbent blend product comprising a zeolite blended with a highlydispersed attapulgite binder, wherein the tapped bulk density of thehighly dispersed attapulgite binder is more than about 550 g/l.
 6. Theprocess of claim 5 wherein the zeolite product comprises zeolite X.
 7. Aprocess for adsorption of carbon dioxide from an air stream comprisingpassing the air stream over a molecular sieve adsorbent blend productproduced by a process comprising preparing a zeolite product; preparingan attapulgite binder comprising highly dispersed attapulgite fibers;mixing the zeolite with the attapulgite binder and water to produce amixture; and forming a molecular sieve adsorbent product from themixture; wherein the tapped bulk density of the highly dispersedattapulgite fibers, as measured according DIN/ISO 787, is more thanabout 550 g/l.
 8. The process of claim 7 wherein the zeolite productcomprises zeolite X or zeolite Y.
 9. A process for removal of water froma gaseous or liquid ethanol stream comprising passing the gaseous orliquid ethanol stream over a molecular sieve adsorbent blend produced bya process comprising preparing a zeolite product; preparing anattapulgite binder comprising highly dispersed attapulgite fibers;mixing the zeolite with the attapulgite binder and water to produce amixture; and forming a molecular sieve adsorbent product from themixture; wherein the tapped bulk density of the highly dispersedattapulgite fibers, as measured according DIN/ISO 787, is more thanabout 550 g/l.
 10. A process for separation of nitrogen and oxygen froman air stream comprising passing the air stream over a molecular sieveadsorbent blend produced by a process comprising preparing a zeoliteproduct; preparing an attapulgite binder comprising highly dispersedattapulgite fibers; mixing the zeolite with the attapulgite binder andwater to produce a mixture; and forming a molecular sieve adsorbentproduct from the mixture; wherein the tapped bulk density of the highlydispersed attapulgite fibers, as measured according DIN/ISO 787, is morethan about 550 g/l.
 11. A process for removal of sulfur and oxygencontaining compounds from a hydrocarbon stream comprising passing thehydrocarbon stream over a molecular sieve adsorbent blend product by aprocess comprising preparing a zeolite product; preparing an attapulgitebinder comprising highly dispersed attapulgite fibers; mixing thezeolite with the attapulgite binder and water to produce a mixture; andforming a molecular sieve adsorbent product from the mixture; whereinthe tapped bulk density of the highly dispersed attapulgite fibers, asmeasured according DIN/ISO 787, is more than about 550 g/l.
 12. Aprocess for removal of carbon monoxide, carbon dioxide and nitrogen froma hydrogen gas stream comprising passing the hydrogen gas stream over amolecular sieve adsorbent blend produced by a process comprisingpreparing a zeolite product; preparing an attapulgite binder comprisinghighly dispersed attapulgite fibers; mixing the zeolite with theattapulgite binder and water to produce a mixture; and forming amolecular sieve adsorbent product from the mixture; wherein the tappedbulk density of the highly dispersed attapulgite fibers, as measuredaccording DIN/ISO 787, is more than about 550 g/l.
 13. A process forremoval of water from a gaseous or liquid hydrocarbon stream comprisingpassing the gaseous or liquid hydrocarbon stream over a molecular sieveadsorbent blend produced by a process comprising preparing a zeoliteproduct; preparing an attapulgite binder comprising highly dispersedattapulgite fibers; mixing the zeolite with the attapulgite binder andwater to produce a mixture; and forming a molecular sieve adsorbentproduct from the mixture; wherein the tapped bulk density of the highlydispersed attapulgite fibers, as measured according DIN/ISO 787, is morethan about 550 g/l.
 14. A process to separate n-paraffins from a mixtureof iso-paraffins and n-paraffins comprising passing the mixture over amolecular sieve adsorbent blend produced by a process comprisingpreparing a zeolite product; preparing an attapulgite binder comprisinghighly dispersed attapulgite fibers; mixing the zeolite with theattapulgite binder and water to produce a mixture; and forming amolecular sieve adsorbent product from the mixture; wherein the tappedbulk density of the highly dispersed attapulgite fibers, as measuredaccording DIN/ISO 787, is more than about 550 g/l.
 15. The process ofclaim 14 wherein the zeolite product comprises zeolite A.
 16. A processfor removal of water from a gaseous or liquid stream of refrigerantscomprising passing the gaseous or liquid stream over a molecular sieveadsorbent blend produced by a process comprising preparing a zeoliteproduct; preparing an attapulgite binder comprising highly dispersedattapulgite fibers; mixing the zeolite with the attapulgite binder andwater to produce a mixture; and forming a molecular sieve adsorbentproduct from the mixture; wherein the tapped bulk density of the highlydispersed attapulgite fibers, as measured according DIN/ISO 787, is morethan about 550 g/l.
 17. A process for removal of water and carbondioxide from air comprising passing the air over a molecular sieveadsorbent blend produced by a process comprising preparing a zeoliteproduct; preparing an attapulgite binder comprising highly dispersedattapulgite fibers; mixing the zeolite with the attapulgite binder andwater to produce a mixture; and forming a molecular sieve adsorbentproduct from the mixture; wherein the tapped bulk density of the highlydispersed attapulgite fibers, as measured according DIN/ISO 787, is morethan about 550 g/l.
 18. The process of claim 17 wherein the zeolitproduct comprises zeolite X or zeolite Y.